• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
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  • 引用文献
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  • 优先权
    • 专利摘要:
    Distillates are produced from asphaltenes-containing hydrocarbon mixtures by a process comprising subjecting the hydrocarbon mixtures to thermal cracking, and subjecting the resulting heavy fraction to a combination of a catalytic hydrotreatment and a solvent deasphalting.
    公开号:SU1424740A3
    申请号:SU833568910
    申请日:1983-03-16
    公开日:1988-09-15
    发明作者:Бартелд Квант Питер；Роберт Ньюсом Джон
    申请人:Шелл Интернэшнл Рисерч Маатсхаппий Б.В. (Фирма)；
    IPC主号:
    专利说明:

    4: GO
    four:
     CM
    The invention relates to a process for the production of distillate hydrocarbon fractions from asphaltene-containing hydrocarbon oil.
    The purpose of the invention is to increase the yield of target products.
    Embodiments of the invention are further sub-divided according to whether the heavy fraction from the thermal cracking treatment product is used as a starting material, or a component of the starting material for catalytic hydroprocessing (NT) (class IIIA), or as a starting material, or a component of a starting material for treatment of dissolving deasphalting (YES) (class IIIB). In the variant belonging to class IIIA, the heavy fraction extracted from the product of catalytic hydrotreatment (NT) is used as a starting material for processing solvent deasphalting (YES). In the embodiments belonging to class II1B, the asphalt bitumen fraction is used as catalytic hydrotreating (NT) feedstock, and the heavy fraction from the catalytic hydrotreating (NT) product is used as a component of the starting material for heat treatment king, or as a component of the starting material for treatment of dissolving deasphalting (DA), individually or in combination with these treatments.
    In the proposed process, the raw material used is a hydrocarbon mixture containing asphaltenes. A suitable parameter for estimating the content of asphaltenes in a hydrocarbon mixture, as well as reducing the content of asphaltenes, which appears when the hydrocarbon mixture containing asphaltenes is subjected to catalytic hydrotreatment (NT), is the RCT test value. A higher content of asphaltenes in the hydrocarbon mixture gives a higher value of the Ramsbottom (RCT) coke sample. Preferably, this process is applied to hydrocarbon mixtures that boil at temperatures substantially higher than 350 ° C and 35 °.
    0
    five
    0
    five
    0
    five
    0
    five
    100 wt.% Of which boils at Bbraie temperatures of 520 ° C and which have a value of a Cox sample according to Remsbottom 7.5-50 wt. Examples of such hydrocarbon mixtures are residues obtained during the distillation of various types of crude oil, as well as heavy hydrocarbon mixtures derived from oil shale and butuminous sand. If required, this process can also be applied to heavy crude mineral oils, residues from thermal cracking of hydrocarbon mixtures, and asphalt bitumen obtained from solvent-based asphaltenes from hydrocarbon mixtures.
    Hydrocracking is carried out at 300 -, in particular at 350-450 s, pressure 50-300 bar, in particular 75-200 bar, volume equilibrium rate 0.02-10 g X g X, in particular 0.1-2 g XX, and with the ratio H, the base material is 100-5000 Nl x X kg, in particular 500-2000 Nl x
    X KG.
    The second or third step is deasphalting, in which the raw material containing asphaltenes is converted into a product from which the deasphalted oil is separated into a fraction and an asphalt bituminous fraction. Suitable solvents for deasphalting are paraffin hydrocarbons having 3 to 6 carbon atoms per molecule, such as p-butane, and mixtures thereof, such as mixtures of propane and p-butane, and mixtures of p-butane and p-pentane. Suitable weight ratios of solvent: the oil lies within (7: 1) - (1: 1), in particular between 4: 1 and 1: 1. The deasphalting (YES) treatment is carried out at a pressure of 20-100 bar. When p-butane is used as a solvent, deasphalting is carried out at a pressure of 35-45 bar and at a temperature of 100-150 C.
    Three technological schemes for the production of distillates of petroleum oils from asphaltenes containing hydrocarbon mixtures according to the proposed method are explained in more detail below.
    Technological scheme A.
    The process is carried out in a system containing successively a thermal cracking zone composed of a thermal cracking unit, a distillation unit at atmospheric pressure, a second thermal cracking unit, a second distillation unit at atmospheric pressure and a vacuum distillation unit, a catalytic hydrotreating zone composed of catalytic hydroprocessing, a third distillation unit at atmospheric pressure, and a second vacuum distillation unit and a dissolving deasphaltine zone Vani. The asphaltenes-containing hydrocarbon mixture is mixed with a stream of asphalt bitumen and this mixture is subjected to thermal cracking. The resulting thermal cracked product is separated by distillation at atmospheric pressure into a gas fraction obtained by distillation at atmospheric pressure distillate and residue. The residue obtained by distillation at atmospheric pressure is mixed with the residue obtained by distillation at atmospheric pressure and this mixture is separated by vacuum distillation into a vacuum distillate and a vacuum residue. The vacuum residue is subjected to catalytic hydroprocessing along with hydrogen. The hydrotreated product is separated by distillation at atmospheric pressure into a gas fraction obtained by distillation at atmospheric pressure, the distillate and the residue. The residue obtained by distillation at atmospheric pressure is separated by vacuum distillation into a vacuum distiller and a vacuum residue. The vacuum residue is separated by dissolving deasphalting into deasphalted oil and asphalt bitumen. De-asphalt oil is subjected to thermal cracking. The thermally cracked product is separated by distillation at atmospheric pressure into a gas fraction obtained by distillation at atmospheric pressure and a residue obtained by distillation at atmospheric pressure. Gas fractions are combined to form the mixture. Asphalt bitumen is divided into two hours.
    ti.
    I
    Technological Scheme B. The process is carried out in the same system and in the same way as described in techno 5 s 0 g -
    five
    logic diagram A, but the asphalt bitumen stream is mixed with the stream instead of the stream.
    Technological scheme C.
    The process is carried out in the system, successively containing a thermal cracking zone composed of a thermal cracking unit, a distillation unit at atmospheric pressure, a second thermal cracking unit, a second distillation unit at atmospheric pressure and a vacuum distillation unit, solvent deasphalting eon and zone catalytic hydroprocessing, composed of a catalytic hydroprocessing unit, a third distillation unit at atmospheric pressure and a second vacuum distillation unit Novki. The asphaltenes-containing hydrocarbon mixture is subjected to thermal cracking and the product obtained by thermal cracking is separated by distillation at atmospheric pressure into a gas fraction obtained by distillation at atmospheric pressure and the residue obtained by distillation at atmospheric pressure. The resultant distillation at atmospheric pressure is mixed with the resultant distillation at atmospheric pressure, and this mixture is separated by vacuum distillation into a vacuum distillate and a vacuum residue. The vacuum residue is mixed with the vacuum residue and this mixture is separated by dissolving deasphalting into deasphalted oil and asphalt bitumen. Asphalt bitumen is divided into two parts. The part is subjected, together with hydrogen, to catalytic hydroprocessing. The product obtained by hydrotreating is separated by distillation at atmospheric pressure into a gas fraction obtained by distillation at atmospheric pressure and distilled to a residue obtained by distillation at atmospheric pressure. The atmospheric residue is separated by vacuum distillation into a vacuum distillate and a vacuum residue. Deasphalted oil is subjected to thermal cracking. The resulting thermal cracked product is separated by distillation at atmospheric pressure into
    the gas fraction obtained by distillation at atmospheric pressure is distilled and the residue obtained by distillation at atmospheric pressure. Gas fractions are pooled. The distillates obtained by distillation at atmospheric pressure are combined.
    Example 1. Carried out according to the technological scheme A. 100 p.p. vacuum residue, ime tse value coke
    The initial mixtures used by Remsbottom 20.2 wt.% Yield
    In the proposed process, there are two asphaltene-containing hydrocarbon mixtures obtained as residues from vacuum distillation from distillation residues at atmospheric pressure from SF mineral oils. Both vacuum residues are boiled at a temperature of 520 ° C. They are Rothbottpm coke (RCT) values. ) 20.2 and 10.1 wt.%, Respectively. The process is carried out according to the technological schemes A - C. The following conditions are used in different zones.
    In all technological schemes, the installation for catalytic hydrotreatment contains two reactors, the first of which is filled with Ni / V / SiO — a catalyst containing 0.5 parts per volt (rf) nickel and 2.0 hours. pv vanadium at 100 ppt. silicon dioxide, and the second reactor, which is filled with a Co / Mo / AljOj catalyst containing 4 p.p. alumina, these catalysts are used in a 1: 4 volume ratio. The catalytic hydroprocessing is carried out at a hydrogen pressure of 150 bar, the weight feed rate per unit of catalyst weight (measured for both reactors) kg of starting material per liter of catalyst per hour, the ratio of N / starting material is about 1000 Nl per kg and the average temperature is 410 ° C in the first reactor and 385 C in the second reactor.
    In all technological schemes, the treatment of dissolving deasphalting is carried out using n-butane as a solvent, at 115 ° C, a pressure of 40 bar and a weight ratio of solvent: oil 3: 1,
    In all technological schemes, thermal cracking is carried out in two cracking coils, at a pressure of 20 bar, a volume-weight rate of 0.4 kg of fresh raw material per liter of cracking coil volume per minute, and temperature
    480 С
    4954
    in the first cracking coil and in the second cracking coil (temperatures were measured at the outputs of the cracked coils).
    Example 1. Carried out according to the technological scheme A. 100 p.p. vacuum residue, ime tse value coke

    50
    five
    different streams of liquids c.p.: Ct-C gaseous fraction Mixture of flows, which was important for a sample of coke according to Remsbottom 23.5 wt.% 350 ° C atmospheric residue Mixture (321)
    The following vacuums are
    five
    0
    five
    0
    350-520 Ny
    distillate 520 ° С vacuum residue having a value of a sample for coke according to Remsbottom 30.8 wt.% of product (324), С, fraction of which had a value of test for coke according to Remsbottom 15.4 wt.% Su - 350 ° C atmospheric distillate
    350 atmospheric residue 350-520 С vacuum distillate 520 ° С vacuum residue
    Deasphalted oil Asphalt bitumen Cj. - 350 ° C atmospheric distillate atmospheric residue Part Part
    8.4
    118.0
    93.6 102.8
    19.5
    83.3
    12.7 68.8
    22.2 46.6
    18.6 28.0
    25.4
    9.2 18.0 10.0
    Example 2, embodied according to the technological scheme B.
    100 h, p. vacuum residue having a coke sample value
    to 20 wt.%, give an output of various flows in the following quantities, ch.p.v .: Gaseous
    fraction 3.32 350 ° C atmospheric residue 82.2 Mixture98.9
    350-5204 vacuum distillate 18.4 520 ° С vacuum residue 80.5
    The mixture of streams, which is the value of the sample for coke according to Remsbottom, is 31.2 wt.% Of the product. Su, the fraction of which is important for a coke test according to Remsbottom 15.6 masl 101.0 С, is 350 ° С atmospheric distillate 16.8 atmospheric residue 78.2
    350-520 s vacuum distillate 25.5 520 ° С vacuum o statok52,7
    Deasphalted oil26,9
    Asphalt bitumen 25.8; C5 - C50 with atmospheric distillate t 24.7 350 C atmospheric residue Part
    Part
    Example 3. In-process flow with
    100 h, p. Vacuum-relevant Remsbottom 10.1 May L sample, various flows in the wakes, ch.p.w .: Gaseous fraction С, -С4 350 С atmospheric residue Mixture
    350-520 ° С vacuum distillate 520 ° С vacuum residue


    IN 1IPI Order 4701/59 Circulation 464
    Random polygons pr-tie, Uzhgorod, st. Project, 4
    five
    0
    five
    0
    Mixture118,2
    Deasphalted oil68,6 Asphalt
    bitumen 49,6
    Part 8,2
    The part that mattered the Cox test according to Remsbottom 38.6 May L product, C, the fraction of which has the meaning of coke test according to Remsbottom
    May 21.2 L41.4
    Su - 350 ° С atmospheric distillate t 5.9 350 ° С vacuum distillate t30.9
    350-520 ° С vacuum distillate 8.1 520 ° С vacuum residue22.8
    权利要求:
    Claims (1)
    [1]
    WITH; - 350 atmospheric distillate 39.1 350 ° C atmospheric residue42.6 Formula of the invention
    n and
    ;
    35
    oh whether
    40
    45
    50
    55
    A method of producing distillate hydrocarbon fractions by processing heavy hydrocarbon feedstock containing asphaltenes, which includes the steps of thermal cracking, deasphalting, and catalytic hydroprocessing, characterized in that, in order to increase the yield of the target products, from thermal cracking products containing 3.3 8.4 wt.% Of the fraction C, -C, the distillate fractions and the cracking residue are separated, which is supplied either at the deasphalting stage, followed by feeding of the deasphalted product to the thermal cracking stage and lennoy asfaltobitumnoy fraction in step the catalytic hydrotreatment or for the catalytic hydrotreatment stage with separation of the products obtained in distillate fractions and a residual fraction which is fed to the deasphalting step of supplying a deasphalted product in the thermal cracking step.
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    引用文献:
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